US3617550A - Method and apparatus for the concentration of solutions - Google Patents

Method and apparatus for the concentration of solutions Download PDF

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Publication number
US3617550A
US3617550A US864309A US86430969A US3617550A US 3617550 A US3617550 A US 3617550A US 864309 A US864309 A US 864309A US 86430969 A US86430969 A US 86430969A US 3617550 A US3617550 A US 3617550A
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United States
Prior art keywords
solution
membrane
membranes
feed solution
rejection
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US864309A
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English (en)
Inventor
Chaim Elata
Jonatan Ben-Dror
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
T-HYDRONAUTICS Inc A CORP OF TX
Tracor Hydronautics Inc
Original Assignee
Hydronautics
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Filing date
Publication date
Application filed by Hydronautics filed Critical Hydronautics
Priority to DE19702046055 priority Critical patent/DE2046055C/de
Priority to ES383820A priority patent/ES383820A1/es
Priority to CH1410270A priority patent/CH517505A/de
Priority to NL7014595A priority patent/NL7014595A/xx
Priority to FR7035995A priority patent/FR2065053A5/fr
Priority to IT3067370A priority patent/IT1065411B/it
Priority to BE757206A priority patent/BE757206A/fr
Application granted granted Critical
Publication of US3617550A publication Critical patent/US3617550A/en
Assigned to T-HYDRONAUTICS, INC., A CORP. OF TX reassignment T-HYDRONAUTICS, INC., A CORP. OF TX ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: HYDRONAUTICS, INCORPORATED A CORP. OF MD
Assigned to TRACOR HYDRONAUTICS reassignment TRACOR HYDRONAUTICS CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). Assignors: T-HYDRONAUTICS, INC.
Assigned to TORONTO-DOMINION BANK, THE, AS AGENT reassignment TORONTO-DOMINION BANK, THE, AS AGENT SECURITY INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TRACOR, INC.,
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23B—PRESERVATION OF FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES; CHEMICAL RIPENING OF FRUIT OR VEGETABLES
    • A23B2/00—Preservation of foods or foodstuffs, in general
    • A23B2/90—Preservation of foods or foodstuffs, in general by drying or kilning; Subsequent reconstitution
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
    • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof containing fruit or vegetable juices
    • A23L2/08—Concentrating or drying of juices
    • A23L2/082—Concentrating or drying of juices by membrane processes
    • A23L2/085—Concentrating or drying of juices by membrane processes by osmosis, reverse osmosis, electrodialysis

Definitions

  • ABSTRACT A feed solution containing a solute and a solvent is concentrated by reverse osmosis.
  • the feed solution is subjected to a given working pressure and is first forced through a series of high rejection membranes.
  • the diluted solution which permeates the high rejection membranes is discarded and the product solution leaving the high rejection membranes is then passed as a feed solution through a series of low rejection membranes.
  • the dilute solution which permeates through the low rejection membranes is preferably recycled to the starting feed solution, but can be discarded, if desired.
  • the product comprises the concentrated solution which does not permeate the low rejection membranes.
  • the working pressure of the solution fed to both the high rejection membrane and the low rejection membranes should exceed R1r' where: R is the rejection ratio of the membrane and 1r is the osmotic pressure of the solution being fed to the membrane.
  • the present invention relates to a new and improved system for the concentration of solutions, and more particularly, to a new and improved method and apparatus for concentrating solutions by reverse osmosis.
  • the hydraulic flow rate of the water can be related to an effective pressure head which is proportional to the concentration of the solution and is called the osmotic pressure of the solution.
  • hydraulic flow can be slowed down by increasing the hydrostatic head on the solution side.
  • the hydrostatic head becomes equal to the osmotic pressure, no flow occurs, and when the hydrostatic head exceeds the osmotic pressure, the flow is reversed and the water now passes from the solution to the fresh water side of the separating membrane.
  • the solution to be concentrated containing a solvent and a solute will be called a feed solution" and the concentrated solution obtained during the concentration process will be called product solution.”
  • the feed solution is placed in contact with a semipermeable membrane, i.e., a membrane through which water may flow but which is s substantially impervious to any solutes such as sugars, organic esters and electrolytes, and a pressure is applied to the feed solution, which is larger than its osmotic pressure,
  • a semipermeable membrane i.e., a membrane through which water may flow but which is s substantially impervious to any solutes such as sugars, organic esters and electrolytes
  • a concentrated product solution usually has a high osmotic pressure.
  • very high hydrostatic pressures that exceed the osmotic pressure of the product solution must be applied in order to obtain concentrated products.
  • Presently available membranes undergo rapid compaction when subjected to such high pressures and suffer a simultaneous loss in flux (permeability rate). This compaction reduces the useful life of the membrane and can significantly affect the cost of concentrating solutions if frequent replacement of membranes is made necessary.
  • a related problem is the capital expense required to construct an entire system capable of withstanding the high pressures.
  • the present invention is based on a method for the concentration of a feed solution by way of reverse osmosis in which the product solution produced by the method is characterized by an osmotic pressure that is higher than the sum of the highest hydrostatic working pressure applied to the feed solution and the osmotic pressure of the solution that permeates through the reverse osmosis membranes and is discarded.
  • the invention also provides a method in which the volumetric flows are minimized so that only a relatively small area of membrane is needed to produce a desired volume of product per day.
  • a feed solution to be concentrated is passed in succession through two series of membranes; the first series of membranes being composed of high rejection membranes and the second series of membranes being composed of high rejection membranes.
  • the present invention also comprises an apparatus including a high rejection membrane or preferably a plurality of high rejection membranes in series which first received the feed solution and separate the feed solution into a concentrated feed solution which does not pass through the membranes and a solvent solution which permeates through the membranes; means for passing the concentrated feed solution to a plurality of low rejection membranes which separate the concentrated feed solution into a product solution which does not pass through the second stage of low rejection membranes and a dilute solution which permeates through the low rejection membranes.
  • the apparatus also includes means for applying and adjusting the working pressure within the membranes; supply means for feeding the feed solution to the high rejection membranes; removal means for disposing of the solvent solution that permeates through the high rejection membranes; and means for collecting and withdrawing the concentrated product solution that has not passed through the low rejection membranes.
  • Means are also provided for either removing and disposing of the dilute solution that permeates through the low rejection membranes or for recycling it to the feed solution.
  • the drawing is a schematic flow sheet of an apparatus for carrying out the method of the invention.
  • -Jv water flux i.e., the number of gallons of solvent, for example, water that pass through i square foot of the membrane per day;
  • Lp volume permeability coefficient i.e., number of gallons of solution permeating through 1 square foot per day under a pressure of l p.s.i.
  • the dimensions of the membranes and chosen to trating a feed solution wherein the feed solution while being reflect the volume and degree of concentration desired for the subjected to a certain working pressure is first passed through specific feed solution to be concentrated. aseries of high rejection membranes.
  • the diluted solution per- The method of the present invention can be used for the meating through the membranes is discarded and the product concentration of any feed solution to a product solution havsolution leaving the high rejection membrane is, while still ing an osmotic pressure which is larger than the highest being subjected to a working pressure, passed as feed solution required working pressure.
  • Typical feed solutions include for through a series of low rejection membranes. example, fruit juices, such as orange juice, strawberry juice,
  • the product solution is collected and the diluted solution and apple uice, and dilute sugar solutions. permeating through the low rejection membranes can be
  • the method of the invention can be performed batchwise or discarded,or preferably, recycled to the starting feed solution. continuously, the latter being preferred.
  • te-lect'vtty of the h teletfttoh methbtahes t be An embodiment of an apparatus according to the present t than that of the tohowthg sehes 0t t h h invention is illustrated inthe accompanying drawing.
  • the vari- Jecttoh memthahes are those thembranles m wh'ch a maxlmum ous parts of the apparatus can be constructed from a variety of h z h i healt y percent t materials that are compatible with the various ingredients of on r g, pure zigg gia the solution and that can withstand the working pressures.
  • the apparatus comprises a feed tank 10, a high pressure .Sute o t e pro so near y equa S e wor pump 12, a high rejection membrane system 14, a low rejecing pressure applied.
  • tion membrane system 16 a product tank T8, and a water tank
  • Low re ection membranes allow some dissolved solids to 20.
  • the pressures within the membrane systems 14 and 16 are permeate through the membrane with the solvent. in this case t d b 22 d 24 l R l and the feed solution, which has been already concen- :de il lh zz Jus m3 g gf ah I lr ytrated to a certain extent in the first stage, i.e., within the high f h as me are 6 a ⁇ f' t e ute rejection membranes, can be concentrated until the new Rqr' tom System 16 to tank 1 elves e also P of the low rejection membranes again neafly equals the work vided for controlling the flow of the solutions at various stages ing pressure in the apparatus and an air accumulator 27 IS positioned ust
  • the solids permeability rate'the low rejection membrane 40 t P can vary
  • the product solution On the other hand, the higher the required concentration of from low rejection membrane system 16 is collected in tank the final product solution (and thus its osmotic pressure), the 18.
  • the feed solumore permeable the low rejection membranes should be. tion is continuously added to tank 10 through line 28 and the Preferably, the amount of dissolved solids retained should at r du t l ti in tank 18 and the olv t i t k 20 are conleast equal the amount of solids permeating through the ti l removed.
  • second stage membrane with the sol e t Second stage membrane with the sol e t.
  • the membrane should be insoluble and chemically EXAMPLES inert in relation to the solvent and all the ingredients of the In these mpl cellulose acetate m m r w e solution.
  • Cellulose acetate membranes which are commerin the apparatus described in the accompanying drawing and cially available, a presently preferred.
  • the membranes may pressure and concentration measurements were performed at have any suitable shape, for example, the membranes may be the points marked on the drawing. tubular or be flat.
  • a series of tubular membranes having their The results of the concentration, pressure, and flux meaends connected forms a preferred high rejection membrane surements are shown in table 1 below, where:
  • the high pressure series of membranes 14 comprises 36 tubular h inches inside diameter membranes aligned in series and the low-pressure membrane 16 also comprises 36 tubular 1% inches diameter membranes.
  • the effectiveness of the new method and apparatus is readily understood from the results of the Examples.
  • the invention permits concentrating feed solutions to obtain a product solution which has a higher osmotic pressure than the sum of the highest hydrostatic working pressure applied to the solution,
  • the invention permits operating at both desirable pressure levels to avoid membrane compaction and a desirably low ration of volume of solvent passed through the membranes per volume of product recovered.
  • the latter characteristic helps reduce the area of membrane required to obtain apparatus having a given product capacity.
  • a method for concentrating a feed solution comprising: forcing a feed solution through a high rejection membrane by subjecting the feed solution to a first working pressure, the diluted solution permeating through the membranes being discarded; forcing the concentrated solution which does not pass through the high rejection membrane and which is still being subjected to a second working pressure as a feed solution to a second membrane having a solid rejection rate that is lower than the rejection rate of the high rejection membrane;
  • An apparatus for concentrating a feed solution comprising: a high rejection membrane which receives the feed solution and separates the feed solution into a concentrated feed solution which does not pass through the membrane, a low rejection membrane which receives the concentrated feed solution that does not pass through the high rejection membrane and separates the concentrated feed solution into a product solution which does not pass through the second membrane, and a diluted solution which does not pass through the second membrane; means for applying and for adjusting the working pressure within said membranes; supply means for forwarding the feed solution to said high rejection membrane; means for passing the concentrated feed solution to the low rejection membrane product collection means connected to the high pressure side of said low rejection membranes; and removal means for discharging the diluted solution which penneates through the high rejection membranes.
  • the apparatus of claim 6 including means for recycling to the supply means the solution permeating through the low rejection membranes to prevent loss of valuable dissolved solids.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Zoology (AREA)
  • Wood Science & Technology (AREA)
  • Nanotechnology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Nutrition Science (AREA)
  • Health & Medical Sciences (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Non-Alcoholic Beverages (AREA)
US864309A 1969-04-04 1969-10-07 Method and apparatus for the concentration of solutions Expired - Lifetime US3617550A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
DE19702046055 DE2046055C (de) 1969-10-07 1970-09-17 Verfahren zum Einengen von Losungen durch inverse Osmose
ES383820A ES383820A1 (es) 1969-04-04 1970-09-19 Procedimiento para la concentracion de soluciones.
CH1410270A CH517505A (de) 1969-04-04 1970-09-23 Verfahren zum Konzentrieren einer Speiselösung zu einer Endlösung und Einrichtung zur Durchführung des Verfahrens
NL7014595A NL7014595A (de) 1969-04-04 1970-10-05
FR7035995A FR2065053A5 (en) 1969-04-04 1970-10-06 Concentration of fruit juices and sugar solns
IT3067370A IT1065411B (it) 1969-04-04 1970-10-07 Metodo ed apparecchio per la concentrazione di soluzioni mediante osmosi inversa
BE757206A BE757206A (fr) 1969-04-04 1970-10-07 Methode et appareil pour la concentration de solutions

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
IL31953A IL31953A (en) 1969-04-04 1969-04-04 Method for the concentration of solutions by reverse osmosis and an apparatus for the performance of said method

Publications (1)

Publication Number Publication Date
US3617550A true US3617550A (en) 1971-11-02

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US864309A Expired - Lifetime US3617550A (en) 1969-04-04 1969-10-07 Method and apparatus for the concentration of solutions

Country Status (8)

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US (1) US3617550A (de)
BE (1) BE757206A (de)
CH (1) CH517505A (de)
ES (1) ES383820A1 (de)
FR (1) FR2065053A5 (de)
IL (1) IL31953A (de)
IT (1) IT1065411B (de)
NL (1) NL7014595A (de)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3788474A (en) * 1970-10-12 1974-01-29 Rhone Poulenc Sa Apparatus for concentrating a liquid containing non-ultrafiltrable elements
US3917526A (en) * 1974-04-04 1975-11-04 Universal Oil Prod Co Combined foam flotation and membrane separation processing
USB524806I5 (de) * 1974-11-18 1976-03-02
EP0070059A1 (de) * 1981-07-10 1983-01-19 Nederlandse Organisatie voor toegepast-natuurwetenschappelijk onderzoek TNO Verfahren und Vorrichtung zur Konzentrierung von Lösungen durch Umkehrosmose
US4875980A (en) * 1986-09-02 1989-10-24 Mitsubishi Rayon Engineering Co., Ltd. Method for separating and concentrating an organic component from an aqueous solution containing same
US4900402A (en) * 1986-03-25 1990-02-13 Kernforschungszentrum Karlsruhe Gmbh Pervaporation process of separating a liquid mixture
US4933197A (en) * 1989-06-07 1990-06-12 Separasystems Lp Process to make juice products with improved flavor
US4959237A (en) * 1989-06-07 1990-09-25 E. I. Du Pont De Nemours And Company Reverse osmosis concentration of juice products with improved flavor
EP0404057A1 (de) * 1989-06-19 1990-12-27 Director Of National Food Research Institute Ministry Of Agriculture, Forestry And Fisheries Konzentration einer Lösung durch Reversosmoseverfahren
WO1991010373A1 (en) * 1990-01-19 1991-07-25 Bush Boake Allen Limited Flavour concentrates and their production
US20080087603A1 (en) * 2006-07-10 2008-04-17 Christopher Heiss Fluid Purification Methods and Devices
WO2011029110A1 (de) 2009-09-11 2011-03-17 Technische Universität Wien Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen
WO2013017628A1 (fr) * 2011-08-02 2013-02-07 Veolia Water Solutions & Technologies Support Installation de traitement d'eau par osmose inverse comprenant une première passe ayant plusieurs étages

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2540152A (en) * 1949-12-10 1951-02-06 Sol W Weller Recovery of light elemental gases

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2540152A (en) * 1949-12-10 1951-02-06 Sol W Weller Recovery of light elemental gases

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Michaels, Ultrafiltration, a Publication of the Amicon Corporation, March, 1968, 27 pages, pp. 13 25 relied on. *

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3788474A (en) * 1970-10-12 1974-01-29 Rhone Poulenc Sa Apparatus for concentrating a liquid containing non-ultrafiltrable elements
US3917526A (en) * 1974-04-04 1975-11-04 Universal Oil Prod Co Combined foam flotation and membrane separation processing
USB524806I5 (de) * 1974-11-18 1976-03-02
US4000065A (en) * 1974-11-18 1976-12-28 Basf Wyandotte Corporation Method and apparatus for purifying aqueous streams contaminated with organic materials
EP0070059A1 (de) * 1981-07-10 1983-01-19 Nederlandse Organisatie voor toegepast-natuurwetenschappelijk onderzoek TNO Verfahren und Vorrichtung zur Konzentrierung von Lösungen durch Umkehrosmose
US4900402A (en) * 1986-03-25 1990-02-13 Kernforschungszentrum Karlsruhe Gmbh Pervaporation process of separating a liquid mixture
US4875980A (en) * 1986-09-02 1989-10-24 Mitsubishi Rayon Engineering Co., Ltd. Method for separating and concentrating an organic component from an aqueous solution containing same
EP0404390A1 (de) * 1989-06-07 1990-12-27 Separasystems Lp Konzentrieren von Saftprodukten mit einem verbesserten Geschmack durch umgekehrte Osmose
AU628989B2 (en) * 1989-06-07 1992-09-24 Separasystems Lp Reverse osmosis concentration of juice products with improved flavor
EP0402121A1 (de) * 1989-06-07 1990-12-12 Separasystems Lp Verfahren zur Herstellung von Saftprodukten mit verbessertem Geschmack
US4933197A (en) * 1989-06-07 1990-06-12 Separasystems Lp Process to make juice products with improved flavor
US4959237A (en) * 1989-06-07 1990-09-25 E. I. Du Pont De Nemours And Company Reverse osmosis concentration of juice products with improved flavor
EP0404057A1 (de) * 1989-06-19 1990-12-27 Director Of National Food Research Institute Ministry Of Agriculture, Forestry And Fisheries Konzentration einer Lösung durch Reversosmoseverfahren
US5096590A (en) * 1989-06-19 1992-03-17 Director Of National Food Research Institute, Ministry Of Agriculture, Forestry And Fisheries Concentration of solution by the reverse osmosis process
WO1991010373A1 (en) * 1990-01-19 1991-07-25 Bush Boake Allen Limited Flavour concentrates and their production
TR25114A (tr) * 1990-01-19 1992-11-01 Bush Boake Allen Ltd TAT KONSANTRATLARI VE BUNLARIN üRETIMI
US5330654A (en) * 1990-01-19 1994-07-19 Bush Boake Allen Limited Flavor concentrates and their production
US20080087603A1 (en) * 2006-07-10 2008-04-17 Christopher Heiss Fluid Purification Methods and Devices
US8119008B2 (en) * 2006-07-10 2012-02-21 Christopher Heiss Fluid purification methods and devices
WO2011029110A1 (de) 2009-09-11 2011-03-17 Technische Universität Wien Verfahren und vorrichtung zur aufkonzentrierung von wertstofflösungen
WO2013017628A1 (fr) * 2011-08-02 2013-02-07 Veolia Water Solutions & Technologies Support Installation de traitement d'eau par osmose inverse comprenant une première passe ayant plusieurs étages
FR2978755A1 (fr) * 2011-08-02 2013-02-08 Veolia Water Solutions & Tech Installation de traitement d'eau par osmose inverse comprenant une premiere passe ayant plusieurs etages

Also Published As

Publication number Publication date
DE2046055A1 (de) 1971-04-22
BE757206A (fr) 1971-03-16
ES383820A1 (es) 1973-07-16
IT1065411B (it) 1985-02-25
CH517505A (de) 1972-01-15
FR2065053A5 (en) 1971-07-23
IL31953A (en) 1972-11-28
IL31953A0 (en) 1969-06-25
NL7014595A (de) 1971-04-13

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